Refining of hydrocarbons



T. T.x GRAY REFINING OF HYDROCARBONS A 3 Sheets-Sheet 2 Filed Aug. 9, 1926 May 20; 11930. T.T. GRAY 1,759,814

'. Y REFINING OF HYDRQGARBONS Filed Aug- 9, 1926 3 Sheets-Sheet 3 @51W www @7M w@ Patented May 20;.-1930 i UNITED 'STATES PATENT "or-*FICE ../TiomAs a'. GRAY, or ELIZABETH, NEW JERSEY, AssIaNoE 'ro GRAY -rltoc'uassus oortronA'rIoN, or NEWARK, NEW JERSEY, A fonronArIoN or DELAWARE REFIN ING OF HYDROCARBONS vApplication mea August 9, 41926. swarm, 128,007.

This invention relates to the refining of hydrocarbons and more especially '.to the refining of distillates obtained bycracking petroleum or the like.

Cracked distillates containv unsaturated hydrocarbon compounds not present in the oil from which the distillate was obtained. Cerl tain of the hydrocarbon compoundsare veryunstable and possess the property of combining between themselves to form new com'- pounds of considerably higher boiling point. Thenew compounds are known as polymers .and the formation thereof is called polymeri- 'zation. Under ordinary circumstances polymerization takes place' slowl It effects disy coloration of the liquid and orms com ounds which will in time'iproduce a deposito heavy vdark solid or semi-solid material. The unstable unsaturatedhydrocarbons are objec- -tionable because of their tendency to cause gum deposition-on valves, pistons, and the" 4parts of gasoline motors. They are also .un-

desirable constituentsof burning oils.. Be`

fore-cracked hydrocarbon distillates'are ready for the market, some treatment is necessary to remove therefrom the4J undesirable unsaturated hydrocarbon compounds.

" able catalytic agent and has disclosed this method in his .Patent No. 1,340,889. Applicants vco-pending application Serial No. 664,893, filed Sept. 26, 1923,-of which this.

application is a continuation in part, is directed in part to the utilization of heat in the vapor to maintain the catalyst at .a'temper'ature which will prevent excessive condensation of the desired product in the catalyst and to the broad idea of continuous removal of lpolymers during the operation of thefproce'ss as well as to conditioning the vapors for treat-- ment by the removal of-high boiling p'oint constituents therefrom prior to contacting the vapors with the catalyst. When fresh, the catalyst is very efficient inpolynierizin the-unsaturated hydrocarbon' compounds an the product obtained vfrom the process is offhighguality. However,- after 'a period of use the catalyst loses itseifectiveness and eventually has to be renewed to obtain a satisfactory product.

An object ofv his ,invention is so to subject tlie distillate in vapor'form to the catalyst material that the efficiency of the catalyst material used in the polymerizing operation is increased wherebya greater yield of treat- 'ed product is obtainable .with a given amount of catalyst material.

.According to this invention, the distillate may be fractionated by means of any suitable fractionating' device or bubble' tower before being contacted with the catalyst so that only .E the desired fraction, which may be gasoline 65 'of definite boiling range, is treted or the distillate may be partially fractionated before polymerization and the vfractionation completed after polymerizationto produce j the desired product. When a' bubble tower is 70 used. as the fractionating device, the.. product obtained is a fraction having a deiniteboiling range and may be gasoline. The cracked distillate is thus rid of the undesirable-high boiling Vpoint constituents,jwhich, unless re- 75 moved-may have a tendency to shorten the useful life ofthe treating material. The vapor is supplied to the treating material from .the fractionating device at uniform vpressure and temperature, thereby minimizing o era- 8o tional supervislon of the apparatus. ince the temperature is uniform, no heat is lost from the vapor after. the treating material has beenbrought up to vapor temperature eX- cept by radiation. The low and h igh boiling point constituents of the fraction having a deiinite boiling range which may be gasoline pass through the treating material together and vthe higher boiling point constituents which are the harder-to treat are diluted with the more easily treated lower boilingv constituents: Since` the va or is supplied to the treating tower directly From the fractionat'or,

-the uncondensible Vgases normally present in cracked distillate serve to dilute the fraction,

a5 thereby rendering it easier of treatment. than if not so. diluted. As the temperature of the vapor supplied to thetreating material is uniform, there is-substantially no difference etweenl the temperature of. the vapor and 190. f

of the treating material after the .device is in operation,and there is less condensationin the treating material of the less volatile portions. With this arrangement, a higher yield of stable product is obtainable for a given -amount of treating material than heretofore. v l

The treated vapor and the liquid products, comprising' polymers together with whatever condensate has formed in or above'the catalyst are withdrawn either together or separately after contact with the catalyst. The

catalyst is thus kept continuously in proper.

condition to be contacted by the vapor. If the treated vapor and polymers are with- .drawn together they may be subsequently separated in any suitable manner. The polymers and accompanying liquids may be refluxed intothe.. system for redistillation or p1 may be stored for subsequent treatment. The vapor is condensed and the condensate coll lected to be utilized as desired.

tacting the yvapor therewith under a pressure Applicant has discovered that in certain` ifnot all instances, the eficiency of the treating material is materially increased by conconsiderably in excess of atmospheric. T he treating material has a longer effective h fe when the vapor is contacted therewith at superatmospheric pressure than when contacted therewith at atmospheric pressure.

Also the yield oftreated product or a given in the condensate of the vapors. My invention accordingly results in selective polymerization by removing the objectionable or unstable unsaturate's without affecting the unobjectionable constituents of the vapors.

Other objects, novel features and advaner 16 is first charged with treating material tages of the invention will be' apparent from the following specification and accompanying drawings, wherein Figures l, 2, 3, 4 'and 5 'disclose different forms of` apparatus for refining hydrocarbons ,in accordance with the invention.

Referring now to Fig. 1, 10 represents a pressure still of the tube type to which oil to be cracked or,` in the case ot a` rerun operation, previously cracked oil-from a distinct-crackingl unit is supplied through the pipe 1l from l 18 controlled by a valve 19 leads through the bottom of the tower. A layer of heat insulating material 20 preferably surroundsthe tow- 'er 16. From the bottom of the tower 16 a 'pipe 21 controlled by a valve 22 leads to a second fractionator This fractionator is of suitable design further to fractionate the treated distillate to yield the desired fraction, which may be gasoline. pipe 24 controlled by a valve 25 connects they fractionator 23 with a condenser 26. The outlet of the condenser 26 communicates with a pipe 28 leading to a tank 30 which is provided with avent i 31 controlled by the valve 32. A reflux pipe 33 leads fromthe4 fractionating tower 13 to the supply pipe 11 for the still 10 and apump 34 is provided for supplying the pressure necessary to force the reflux into the supply communicates with a p ipe 36 equipped with valves 3-7 and 38 arranged at either side of the connection between the pipe 35 and the pipe 36. From the valve38 the pipe 36 leads to a cooler 39 which in turn communica-tes through a pipe 40 with a tank 42 having avent 43 con- A discharge pipe 35 leads from the Vbottom of the fractionating'device 23 and trolled by af valve 44. Through the valve37 and the pump 45 the pipe 36 communicates 'with the bottom of the'fractionating device 1 13. The shelf 17 supports within the tower 16 a body 46 of treating material or catalytic agent such, for example, as fullers earth,

bauxite, silica gel or other adsorbent material which is capable ot polymerizing unstable unsaturated hydrocarbon compounds v in cracked distillate to form compounds of high-v er boiling point than the temperature of the vapor treated. The treating .agent is pre-l vented from sifting through the perforations in the shelf 17 either by means of screens or layers of mineral wool or similar substances laid upon the shelf.' After the catalyst has become spent it may be removed by bein/g,lr f

drained out-through the spout 18. u

In the operation of this apparatus the towthrough a manhole 29 at the top of the tower and thenoil to be cracked or a cracked distillate from a separate cracking unit is admitted to the still through the pipe 11. The vaporized distillate flows through the pipe 12 aud into the fractionator 13 where it ispartially fractionated. The condensate which may contain some of the desired product is refluxcd through the pipe 33 and pump 34 to the still and the vapor led through t-he pipe' 14 and valve 15 to the tower 16. Here the vapor passes through the treating material which is maintained substantially at the temperature of the vapor as radiation losses are substantially prevented by `the layer of insulating material. In their passage through the treatingl material the unstable unsaturated hydrocarbons present in the vapors are polyi04 the vapor into contact with the treating man lerized into compounds of highervboiling v condensation in the catalyst. They are thus 4continuously withdrawn from the catalyst,

leaving it in proper condition to be contacted A with fresh vapor. The liquid products'and treated vapor are conducted through the pipe s 21 and the valve 22 to the fractionator 23 Y where the liquid products are separatedy fromV 'the treat-edvapor andthe latter is further fractionated to obtain the desired product which'may be gasoline of deiinite boiling range. This product in vapor form is led off through the pipe 24 and valve 25, to the condenser 26 lfrom whence, after condensation, it flows to the tank 30. Permanent gases may be allowed to escape from the product in the tank 30 through the vent pipe 31.V The'liquid products including the polymers drain out through the pipe 3 5 into the pipe 36. By closing the valve 37 and opening the valve 38, the liquid may be led to the cooler 39 and from thence 'to the tank 42. Byclosing the valve 38 and'opening ,the valve 37 the liquid may be returned to the bottom of the fractionatl ing device -13 from whence it is refluxe'd into the system through the pipe 33 vand pump To utilize applicants discovery that a greater eiciency'of treating material is obtained by contacting the treating material with vapor under a pressure considerably in excess of atmospheric, the ltemperature of the still 10 may be regulated and the valves 15,

22, 25 and 32 manipulated-properly to bring terialat any desired pressure. The pressure 7 may be selected at which it has been found lto the treatin material is mosteffective. i The eilf'ective life of the treating material is materially increasedby an increase iii pressure in the va`por and a corresponding increase of yield is obtained in the treated product for a given amount of treating material. By means of the valves a pressure diferential may be obtained in different parts of the system and may be regulated as desired. By proper regulation of the valves the vapor may be brought into contact with the treating material at atmospheric pressure, if desired.

- Referring no 'w to Fig. 2, 10` is `thestill from which the vapors are ledf through the -pipe 12a to the fractionator 133. F ro'm the frac'- tionating tower 13" the vapor-is v conducted perforated conical shelf 17a terminating in aA I ves through the pipe 14.and valve 15EL to, the treating tower 16a in which-is arranged a discharge spoutl 18*A controlled by valve 19a. A ldischarge pipe .21 controlled by valve l22a leads from the bottom.A of the tower-16a toa ing from the still to the fractionating tower condenser 26". The outlet vfrom the condenser leads to a storage tank 30a having a vent 31a controlled by the valve 32a. A reflux pipe 33 leads. from the fractionator 13"` through the pump 34a to the supply pipe 11a `forth@ still 1(). g A layer of insulation 2Oa surrounds t the treating tower 16a and within the tower ator 13a is one capable of yieldingly a fraction having a definite boiling range which fraction may be gasoline. The vapor may be contacted with the treating material under pressure, any desired pressure being obtainable by. regulation of the temperature in the.

still and manipulation of theJ valves 15,'22"*` Y and 32"'.v

VIn Fig. 3, 10" is the still12"ythe pipe lead- 13" and 14" is the pipe controlled by the valve 15" leading to the treating tower 16". 17" is Y the perforated shelf and 18" the discharge spout controlled by valve 19". The'pipe 2 1" controlled by the valve 22" leads to a condenser 26" which in turn leads to a tank 30".' A reflux pipe 47" leads from the'bottom of the treating tower 16" through a pump 48" to the bottom of the fractionator 13". A layer of insulating material 2'()b surrounds the tower 16" and a supply of treating material 46" issupported on the shelf 17". In this apparatus the'treated vapor is withdrawn from the tower16" through the pipe 21" and valve '22" to thecondenser 26" where it is' liquefied and then discharged vinto the storage tank 30". Thev polymers and any condensate are separately removed from the treating tower 16" through the reflux pipe 47" and arefdischarged f into the bottom of the fractionator 13" from whence they are refluxed through the pipe 33". and pump 34" to the feed line 11" of the still 10". By means of the fractionator 13", a fraction of definite boiling range, which may be gasoline, is obtained and is brought linto contactA with the treating material at any desired pressure byfregulation of the temperature of the still 10" and manipulation of the valves 15" a-nd 22".

' Referring non7 to Fig. 4, .10c is the still, 12c 'A the pipe leading from the still to the fracp' tionating tower 13. 14c is the lipe controlled by the valve 15c leading vfrom t e fractionator 'l 13" to thetower '16' -in which is provided -a perforated conical shelf 17 terminating in a discharge spout 18"*controlledby valve 19.

Within the tower 16c a supply of treating' material 46"l is supported upon the shelf 17c and a layervof'ins'ulating material 20c surl rounds the tower. 2lc is a vapor discharge I pipe controlled by the valve 22l leading to the fractionator 23. From the top of the fractionator 23 a pipe-24 controlled by valve 25 leads to a lcondenser 26 and from the condenser apipe 28 leads to a tank30 having a vent pipe31 controlled by valve 32.'v A discharge pipe 47. for liquid products leads from y the bottom of the tower 16 to a pipe 36 equipped with valves 37 and 38. Through the valve 38 the pipe 36 communicates with a cooler 39 which in turn communicates with a.. tank 42. Through the valve 37 and pump 45 the pipe 36 communicates with the bottom of thefractionator 13 from which a reflux pipe 33 leads through the pump 34 to the supply line 11 for'the still 10. A reflux pipe 48 leads from the bottom of the fractionator 23 to the pipe 36 between the valve 37 and pump 45. In this apparatus cracked distillate from lthe still 10 is partially fractionated vand brought into contact with the catalytic agent 46- and polymerilzed.l The treated vapor and liquid products are separately withdrawn from the tower 16. The

vapors are passed through the fractionator 23 where they may be further fractionated and from there to the condenser 26. The condensate collecting in the fractionator 23 may be reiuxed into the system for redistillation. The liquid product from the tower 16 including the polymers may either be collected in the tank 42 by beingrun through the cooler 39 or may be fed back through the fractionator 13 to the still 10. for further re-dis- 'apparatus a pipe -33" controlled by valve 33 leads from the redux pipe and provides means to permit removal of unvaporized residue from the system.

Referring now to Fig. 5, the pressure still set in brick lwork is heated by lire or otherwise in the usualmanner.l It is connected by avapor line 56 to a point near the bottom of the fractionating tower 57. Within the fractionator is mounted a. container 58 which .is open at the top, thereby communicating with the interior of the fractionator and is provided at lits bottom with a restricted neck portion 59 which communicates with a separating chamber 62 mounted within the lower portion of the fractionator. A return line 60 leads from the foot of the fractionator to i. the'still 55. A second vapor line 61 leads i from a point above the bottom of a separating chamber 62 to a condenser 63 and storage tank 65. A pipe 66 leads from the footv of operationof the valves .the chamber 62 to a three-way valve 67, one

connection 68 from which leads back to the still and the other connection 69' to a cooler 70 and tank 71. A vent pipe 72 from the tank isprovided for separating the fixedgases from the condensate. Valves are provided for the pipes 61, 68, 69 and 72. Within the container 58 is provided a body of treating material which is supported upon a perforated partition 76.]'ust above the neck 59 and over which is placed a layer of mineral wool or the like to prevent the treating material falling through the perforations.` Manholes 77 and 78 are provlded for charging-and cleaning the container 58. yIn the operation of this. apparatus the oil to be cracked or a previously cracked oil is charged into the still 55. The oil is heated and distilled'under any desired pressure by regulation of the valve in the pipe 61. The vaporized cracked products enter the fractionator 57 through the pipe 56 and come in contact with and impart heat to the treating material container 58 and to material contained therein. The liquids entrained in the vapors ,and the heavier portions of the vapors which are condensed in the fractionator return to the still .through the pipe 60. The vapors pass 4up and around the container 58 and enter it at the top, passing down through the treating material and lthrough the partition 76 and vneck 59 into the separating chamber 62 and 65. After a period of operation the treat-,

ing material/in the container 58 commences to be wetted at the top due to the formation thereof polymers of higher boilingv point than the temperature of the entering. vapors.

This wetness increasesl progressively downwards towards the bottom of the treating material as the distillation continues until the polymers pass with the vapors through the neck 59 into the chamber .62. The polymers and other liquids flow out through the chamber 62 tothe pipe 66. If it is desired to collect the polymers,'the three-way valve 67 may be set to lead them into the pipe 69 and-to the tank 71. Otherwise they may be returned to the still 55 by the pipe 68. Here again the polymers are continuously drained oil from the treating material! so that it is continuously in proper condition to be contacted with by fresh vapor: The vapor may be brought into 'contact with the treating material at any desired pressure by regulating the temperature in the still 55-and regulatl.

ing the valve in the'pipe 61.

In each form of apparatus described herein the-temperature of the treating material is maintained substantially at'the temperature of the vapor to be treated ysothat excessive condensation is'prevented during the treat-A ing operation'. In the modifications disclosed in Figs. 1v to ltinclusive the layer of insulating Vmaterial surroundin the treating tower prevents loss of heat y radiation andpassage of the vapor through the treating-material heats it substantially to the temperature ofthe vapor. In- Fig. 5 the vapor is brought into heat exchange relation tothe treating material before being'brought into actual contact therewith., The boiling point of the polymers -formed by the action of the treating material on the unstable unsaturated hydrocarbons in the vapor is higher than the temperature of the vapors so that 'upon their formationf-'they condense into liquid form. Polymers drain vthrough the catalytic materia-land drip into the bottom of the tower from which they are continuously drained off, thereby effecting-continuous" separation of the polymers fromv the vapors.

. By reference in the claims to the removal of polymers from the vicinity of the treating zone', I mean removal of polymers. from the treating tower. The catalytic material is thus continuously kept in condition to be contacted with fresh vapor. In each instance advantage may be taken of the applicants discovery that the eiciency ofthe catalytic material is increased when the vapor tobe treated is supplied thereto under pressure in excess of atmospheric. By virtue of this discovery, a greater amount of vapor can .be treated with a given amount of catalyst.

Although applicants invention has been,

disclosed in connection with pressure type cracking units it is not limitedv to such use.

When the invention is used in connection Awith atmospheric pressure type cracking stills, vapor phase cracking stills or in a rerun distillation, the 4vapor may be com-.

pressed by any suitable means before being brought into contact with the catalyst. lWhether or not the vapor is subjected to the inch.

' This process is of particular utility in the and treatingv tower. Extremely good results have been obtained by operating-under pressures llying between 25 and 200 lbs. per square production' of motor' fuel such as gasoline. Cracked distillate treated according' to the method described to remove therefrom the.

Vunsaturated unstable hydrocarbons yields a highA uality'gasoline which isimmediately .available for use in lnternal combustion engines, except in, cases where the cracked products originally contain high amounts of'v sulphur compounds, in which case it maybe desirable to further rene them before, during, or after thetreatment herein disclosed.'

Where o ils are cracked primarily to produce gas the gas may contain `as impurities objectionable polymerizable. hydrocarbons.l

In -such cases'the said objectionable constituents can bel removed by polymerizationin a manner similar to the one herein set forth. The treated vapors would not be condensedbut would be led to a storage tank. The l polymerized material may be reiiux'ed to the v system or may be collected Separately.

By the words solid adsorptive material, solid adsorptive catalyst and. adsorptive catalytic material as used in the appended claims, I intend to include only materialsy of that class Which are capable of selectively polymerizing objectionable` unstable, yunsaturated constituents of cracked hydro-v carbon vapor which tend todiscolor one exposure tolight and to form deposits.

What I claim as new and desire 'to secure by Letters Patent of the United vStates is 1. The method of obtaining substantially color stable motor fuel, whichl comprises resulting cracked vapors to partial condensation to obtain a vapor fraction having a definite boiling range, contacting the'fraccracking a hydrocarbon oil, subjecting the" tion thus obtained'wliile still lin vapor phase with solid adsorptive'gmaterial thereby polymerizing the constituents of the fraction which tend to discolor on exposure toliglit 'and to [form deposits, c'ontinuously draining from said adsorptive material and Withdrawingfrom the vicinity of the treating zone polymers formed in said material, and continuously removing the treated fraction from said adsorptive material.

2. The method of obtaining substantially color stable motor fuel, which comprises vcracking a hydrocarbon oil, obtainingrfrom the cracked distillate a fraction having a definite boiling range, contacting said fraction in vapor phase at super-atmospheric pressure with solid adsorptive material therebypolymerizing the constituents of the fraction which tend to discolor on exposure'to -light and 'to' form deposits, continuously draining'from said adsorptive material and removing from the 4vicinity of the treating zone 'polymers formed in said material and removing the treated fraction from theadsorptive material.

. 3. The method of producing motor fuel y that will not readily polymerize through the ordinary actionrof vlight and air, from hydro-carbon vapors containing unstable, un-

saturated compounds, which consists in obtaining from the'hydrocarbonvapors by partial condensation a vapor fraction having a defnite'boilingfrange, passing the fraction while still in vapor phase into contact with a solid adsorptive catalyst ythereby polymerizing theV constituents of the-fraction which` tend to discolor on exposure to light and to form deposits, continuously drainingfrom said adsorptive material and withdrawing from the vicinity of the treating zone polymers formed in said adsorptive material, and continuously removing the treated fraction from the adsorptive material.

4. The method of obtaining substantially color stable motor fuel which comprises cracking a hydrocarbon'oil, subjecting the resulting'cracked vapors to partial condensation tov obtain a vapor fractionhaving a definite boiling range, contacting the fraction thus obtained while still in vapor phase with solid adsorptive catalytic material to effect polymerization of the constitum., ents of the fraction which tend to discolor`on exposure to light and to form deposits, and continuously draining from said adsorptive material and withdrawing from the vicinity of the treating .zone polymers formed in said material.

5. The method of obtaining substantially .color stable motor fuel, which comprises cracking a hydrocarbon oil, obtaining from the cracked-distillate and in vapor phase a fraction having a definite boiling range, maintaining said fraction in vapor phase and .bringing it intocontact with solid adsorptive material at super-atmospheric pressure 4to effect polymerization of the constituents of 1 the fraction which tend to discolor' on exposure to light and to form deposits, effecting condensation in the adsorptive material of the polymers thus formed, continuously draining from saidv adsorptive material and withdrawing from the vicinity of the treating zone polymers formed in said material, and continuously removing the treated 'frac'- tion from said adsorptive material.

6. The method of obtaining substantially color stable "motor fuel which comprises cracking a hydrocarbon oil, obtaining from.

4the cracked distillate and in vapor phase a fraction having a definite Iboiling range, maintaining said fraction in vapor phase and bringing it into contactl with solid adsorptive material at' super-atmospheric pressure to effect polymerization ofthe constituents of the. fraction'whieh -tend to discolor on exposure to lightand to form deposits, .and vcontinuously draining `from and removing from the vicinity of the treating zon'e polymers thus formed therein.

7. The process of producing substantially color stable gasoline, whichv comprises cracking a hydrocarbon oil, subjecting the resulting ,cracked vapors to partial condensa-` tion to obtain a vapor fraction inthe gasoline boiling range, contacting the fraction thus obtained While still in vapor phase with solid absorptive material to effect polymerization of the constituents of the, fraction which tend to discolor` on exposure to'llght and to form deposits, effecting separatlon of the treated fraction and polymers bypconents of the fraction which tend to discolor' on exposure to light and to form deposits, separating the treated fraction from the polymers thus formed by vcondensation of the latter, and continuously draining from the solid adsorptive material and `removing from the vicinity of the treating zone liquid polymers formed in -the material'.

9. The, method of obtaining substantially color stable motor fuel which comprises cracking a hydrocarbon oil, fractionating the cracked distillate, passing the fraction thus obtained in vapor phase throughfsolid adsorptive material to effect polymerization of the constituents of the fraction which tend to discolor on exposure to light and to form deposits, continuously removing polymers from said material and from the vicinity of the treating zone continuously withdrawing treated vapor from said adsorptive material and separating thel samel from the polymers,

and subsequently fractionating the treatedv vapor to obtain motor fuel having a definite boiling range.

l0. The process of producingfromcracked` distillate motor fuel relatively free from gumV forming constituents and compounds unstable to light, whichlvcomprises Vaporizing said distillate, ,subjecting the vaporized distillate to a fractionating step to 'remove therefrom the portion lying outside the boiling range of gasoline, passing the remaining vapor through a body ofl solid adsorptive material thereby effecting' polymerization of the gum forming constituents and com-` pounds unstable to light, continuously withv drawing polymers fromthe ladsorptive material and from the' vicinity of the treating zone, continuously removing treated vapors and separatmg the Same from the polymers, removmg from the'treated vapor constituentslying outside the desired boiling range and linally condensing thevremainin'g vapor. 11. The process-,of treating cracked distillate for the purpose of producing there- Y from motor fuel relatively free from gumformlng constituents and compounds unstable to light, which comprises vaporizing cracked distillate, subjecting the vap'orized i i color stable-motor carbons, which comprisessubjecting sa1d hydroc'arbons to cracking conditions, remov- 4treated vapor constituents lying outside the desired boiling range and finally condensing the remaining vapor. .y

v 12. The -process of producing. substantially fuelfrom heavy hydroing from 'the evolved vapor, by partial condensation, hydrocarbons lying outside the gasoline boiling range, passing the remaining vapor through a body of solid adsorptive material, thereby effecting polymerization of theconstituents of such vapor whlch tend to discolor on exposure tolight and toformv deposits, continuously withdrawing olymers from the adsorptive material 'and rom the vicinity ofthe treating zone, continuously removing the treated vapor from said adsorptive material and separating it from the polymers, removing vfrom the treated vaporv constituents lying outside'the desired boiling range and ing the remaining vapor.

13. The process of producing substantially color stable .motor fuel from heavy hydrocarbons, which comprises subjecting saidv hydrocarbons to heat and pressure, removing from 4the evolved vapor hydrocarbons lying outside vthe gasoline boiling range, passing the remaining vapor while under super-atmospheric pressure adsorptive material thereby' .polymerizing the constituents of the vapor which tend to discolor on exposure to light andto form deposits, continuously withdrawing -p'olymers from said adsorptive'material and from thevicinity of the treating zone, continuous- 1.. rial and separating it from the polymers, and subsequentlycondensing said vapor.

14. The process-'of obtaining lmotor fuel from crackedhydrocarbons which comprises p fractionating the same to remove hydrocarbons of higher boiling point than the- 4gasoline range, passingthe fractionated vapor in a downward stream through a body of solid. adsorptive catalytic material, thereby polymerizing hydrocarbons which tend to be unstable in the presence of light and to definally condensdraining polymers from the adsorptivematerial with the help of the vapor stream, re-

movingl the treated vapor fromsaid adsorpl tive material, and subsequently collecting and condensing the treated vapor.

In'testimony whereof, Ihave signedmy name to this specification. y

THOMAS-T. GRAY.

through a body of solid l removngthe treated vapor from said maposit* gum, maintaining the adsorptive mation, point ofV such polymers, continuously temperature below the condensa I 

